CN112300818A - Method for preparing bio-oil by coupling biomass pyrolysis and methane aromatization - Google Patents
Method for preparing bio-oil by coupling biomass pyrolysis and methane aromatization Download PDFInfo
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Abstract
The invention discloses a method for preparing bio-oil by coupling biomass pyrolysis and methane aromatization, belonging to the technical field of energy. The method of the invention comprises the following steps: (1) crushing biomass and mixing the crushed biomass with a supported metal catalyst to obtain a mixture; (2) in the methane atmosphere, the mixture obtained in the step (1) is subjected to catalytic pyrolysis reaction at the constant temperature of 600-800 ℃ and under the pressure of 0.1-3.0Mpa for 60-600 min; (3) condensing and collecting the gas obtained by catalytic pyrolysis. The invention reduces the cost of the hydropyrolysis, does not need the participation of an oxidant, and has the yield and the quality of the bio-oil higher than the quality and the yield of the hydropyrolysis bio-oil under the same condition, thereby having important industrial popularization value.
Description
Technical Field
The invention relates to the technical field of energy, in particular to a method for preparing bio-oil by coupling biomass pyrolysis and methane aromatization.
Background
The current society faces the problems of energy shortage, increasingly serious environmental destruction and the like, biomass energy is used as renewable green energy, great development and utilization are of great significance to industry and social life, and a biomass pyrolysis technology is one of effective and feasible methods for converting biomass into biomass energy.
The liquid product obtained by biomass pyrolysis, namely the bio-oil, is an important chemical raw material, the bio-oil contains a large amount of aromatic hydrocarbons and heterocyclic compounds and is a raw material of some special chemical preparations and new chemical materials, however, the bio-oil in the traditional biomass pyrolysis process has low quality and is difficult to directly utilize. Currently, biomass pyrolysis processes for the purpose of improving bio-oil quality and yield are mainly of the following types:
1. acid ion pretreatment: the physical and chemical structures of the biomass can be changed to a certain extent through an acidic ion pretreatment process, so that the aim of improving the quality of the bio-oil is fulfilled; 2. bipolar catalysis method: pyrolyzing biomass by mixing the biomass with an ore catalyst; 3. a hydrogenation pyrolysis method: compared with the conventional condition that pyrolysis is carried out under the inert gas atmosphere, the operation process of pyrolysis under the reducing hydrogen atmosphere has the advantages that the generation amount of unsaturated hydrocarbon under the hydrogen atmosphere is reduced, so that pyrolysis products are mostly condensed in the form of bio-oil, and the purpose of improving the quality of the bio-oil is achieved. The results of the study by Putun et al show that the yield of bio-oil pyrolyzed from bagasse under hydrogen atmosphere can be increased by 40% compared to the case of inert gas atmosphere. (Putun et al, Renewable Energy1994, 5: 816). The Balaguumurthy and the like carry out pyrolysis contrast experiments on rice straws in the hydrogen and nitrogen atmosphere, and the experimental results show that the selectivity of phenolic compounds in the bio-oil is low in the nitrogen atmosphere, the phenolic compounds in the bio-oil have higher selectivity in the hydrogen atmosphere, and the quality of the bio-oil is improved. (Balaguumurthy et al, Bioresour Technol, 2015, 188: 237). 4. Catalytic co-pyrolysis process: the secondary megabyte equally adopts the co-catalytic pyrolysis of biomass and waste polyolefin plastics to improve the hydrogen-carbon ratio of a pyrolysis reactant so as to improve the quality of bio-oil.
But the acid ion pretreatment method and the bipolar catalysis method have higher requirements on reaction conditions, the sources of waste polyolefin plastics in the catalytic co-pyrolysis method are not wide, and the yield and the quality of the bio-oil realized by the method can still not meet the requirements; although the quality and yield of the bio-oil can be obviously improved by the hydropyrolysis process, the hydrogen production cost is high, and the application of the hydropyrolysis process in industrial production is restricted. Therefore, the development of new pyrolysis process instead of hydropyrolysis is a new research direction of biomass pyrolysis technology.
Disclosure of Invention
The invention aims to provide a method for preparing bio-oil by coupling biomass pyrolysis and methane aromatization, which solves the problems in the prior art, can reduce the hydropyrolysis cost and can improve the yield and quality of the bio-oil.
In order to achieve the purpose, the invention provides the following scheme:
the invention provides a method for preparing bio-oil by coupling biomass pyrolysis and methane aromatization, which comprises the following steps:
(1) crushing biomass and mixing the crushed biomass with a supported metal catalyst to obtain a mixture;
(2) in the methane atmosphere, the mixture obtained in the step (1) is subjected to catalytic pyrolysis reaction at the constant temperature of 600-800 ℃ and under the pressure of 0.1-3.0Mpa for 60-600 min;
(3) condensing and collecting the gas obtained by catalytic pyrolysis.
Further, the mass ratio of the supported metal catalyst to the biomass is (0.8-5): 1.
Further, the biomass comprises corn stover, wheat straw, or sweet sorghum stover.
Further, the biomass is crushed and then sieved by a 100-mesh sieve.
Further, the supported metal catalyst is a Mo/HZSM-5 catalyst or a Fe/HZSM-5 catalyst.
Further, the preparation method of the Mo/HZSM-5 catalyst comprises the following steps:
soaking the HZSM-5 powder in an ammonium molybdate solution at room temperature for 18-20 hours, drying at 88-90 ℃ for 8-10 hours, roasting at 540-550 ℃ for 5-6 hours, tabletting and molding, and screening out 20-40-mesh particles to obtain the Mo/HZSM-5 catalyst.
Further, the preparation method of the Fe/HZSM-5 catalyst comprises the following steps:
soaking the HZSM-5 powder in a ferric nitrate nonahydrate solution at room temperature for 22-24 hours, drying at 78-80 ℃ for 10-12 hours, roasting at 540-550 ℃ for 5-6 hours, tabletting and molding, and screening out particles of 20-40 meshes to obtain the Fe/HZSM-5 catalyst.
Further, the methane atmosphere is natural gas or methane gas.
Further, the gas flow rate of the methane atmosphere is 50-36000 ml/min.
The invention discloses the following technical effects:
the invention uses methane as reaction atmosphere to replace pure hydrogen atmosphere for pyrolysis. The methane can react under the action of a catalyst at high temperature without oxygen:
6CH4→C6H6+9H2 ΔH＝-530KJ/mol
free radical reactions such as homolytic cracking and the like can occur in the rapid pyrolysis process of biomass, so that unstable free radical intermediates are generated, and the free radicals can undergo polycondensation and crosslinking reactions to a certain extent. Effectively stabilize the free radical intermediates, thereby reducing the generation of coke, improving the yield and grade of the bio-oil and realizing the high-efficiency conversion of biomass. The invention adopts methane atmosphere to generate small molecular free radical (CH) in methane aromatization process4Activation to form H and CH3Free radicals) that promote stabilization of biomass pyrolysis free radicals, inhibit polycondensation crosslinking reactions between the free radicals, and thereby promote conversion of the biomass.
The aromatization process of the present invention produces a large amount of hydrogen and also produces CHXThe free radical fragments are beneficial to stabilizing free radicals generated by biomass pyrolysis, and the yield and quality of the bio-oil are improved. The invention reduces the cost of the hydropyrolysis, does not need the participation of an oxidant, and has higher yield and quality of the bio-oil than the quality and yield of the bio-oil hydropyrolyzed under the same condition.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.
FIG. 1 is a schematic diagram of the pyrolysis reactor of the present invention;
wherein 1 is a mixture layer formed by a supported metal catalyst and biomass, and 2 is a gas distribution plate; 3 is the inlet of the pyrolysis reactor; and 4 is an outlet of the pyrolysis reactor.
Detailed Description
Reference will now be made in detail to various exemplary embodiments of the invention, the detailed description should not be construed as limiting the invention but as a more detailed description of certain aspects, features and embodiments of the invention.
It is to be understood that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. Further, for numerical ranges in this disclosure, it is understood that each intervening value, between the upper and lower limit of that range, is also specifically disclosed. Every smaller range between any stated value or intervening value in a stated range and any other stated or intervening value in a stated range is encompassed within the invention. The upper and lower limits of these smaller ranges may independently be included or excluded in the range.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. Although only preferred methods and materials are described herein, any methods and materials similar or equivalent to those described herein can be used in the practice or testing of the present invention. All documents mentioned in this specification are incorporated by reference herein for the purpose of disclosing and describing the methods and/or materials associated with the documents. In case of conflict with any incorporated document, the present specification will control.
It will be apparent to those skilled in the art that various modifications and variations can be made in the specific embodiments of the present disclosure without departing from the scope or spirit of the disclosure. Other embodiments will be apparent to those skilled in the art from consideration of the specification. The specification and examples are exemplary only.
As used herein, the terms "comprising," "including," "having," "containing," and the like are open-ended terms that mean including, but not limited to.
The "parts" in the present invention are all parts by mass unless otherwise specified.
FIG. 1 is a schematic diagram of the pyrolysis reactor of the present invention; wherein 1 is a mixture layer formed by a supported metal catalyst and biomass, and 2 is a gas distribution plate.
The natural gas used in the invention is the natural gas which is mined in the oil field and contains methane gas.
Example 1
The biomass used in this example was corn stover, and the industrial and elemental analyses are shown in table 1.
TABLE 1
1. Preparation of Mo/HZSM-5 catalyst
And (2) soaking the HZSM-5 powder in an ammonium molybdate solution at room temperature for 18 hours, drying at 90 ℃ for 10 hours, roasting at 550 ℃ for 6 hours, tabletting and molding, and screening particles of 20-40 meshes to obtain the Mo/HZSM-5 catalyst.
2. Preparation of bio-oil by catalytic pyrolysis
(1) Crushing corn straws, sieving the crushed corn straws with a 100-mesh sieve, and then preparing a catalyst according to Mo/HZSM-5: the corn straw is 5: 1, mixing the two components according to the mass ratio to obtain a mixture;
(2) placing the mixture in a fixed bed pyrolysis reactor, introducing methane gas from an inlet of the pyrolysis reactor at a gas flow rate of 60ml/min, and carrying out catalytic pyrolysis reaction at a constant temperature of 750 ℃ and a pressure of 0.1MPa for 30 min;
(3) liquid products generated by pyrolysis are carried out of the reactor along with gas, the liquid products are collected by a cold trap (-20 ℃), uncondensed gas is analyzed by Agilent gas chromatography (Agilent G1530N), and liquid products are qualitatively detected by GC-MS (Agilent 7890A/5979C). The bio-oil yield thus obtained was 42.3 wt.% and the aromatic hydrocarbon yield was 15.1 wt.%.
Example 2
The biomass used in this example was corn stover, and the industrial and elemental analyses are shown in table 1.
1. Preparation of Fe/HZSM-5 catalyst
And (2) soaking the HZSM-5 powder in a ferric nitrate nonahydrate solution at room temperature for 24 hours, drying at 80 ℃ for 12 hours, roasting at 550 ℃ for 6 hours, tabletting and molding, and screening out 20-40-mesh particles to obtain the Fe/HZSM-5 catalyst.
2. Preparation of bio-oil by catalytic pyrolysis
(1) Crushing corn straws, sieving the crushed corn straws with a 100-mesh sieve, and then preparing a catalyst according to the weight ratio of Fe/HZSM-5: corn stalk is 0.8: 1, mixing the two components according to the mass ratio to obtain a mixture;
(2) placing the mixture in a fixed bed pyrolysis reactor, introducing methane gas from an inlet of the fixed bed pyrolysis reactor at a gas flow rate of 36000ml/min, and carrying out catalytic pyrolysis reaction at the constant temperature of 800 ℃ and the pressure of 3Mpa for 200 min;
(3) liquid products generated by pyrolysis are carried out of the reactor along with gas, the liquid products are collected by a cold trap (-20 ℃), uncondensed gas is analyzed by Agilent gas chromatography (Agilent G1530N), and liquid products are qualitatively detected by GC-MS (Agilent 7890A/5979C). The bio-oil yield thus obtained was 42.2 wt.%, and the aromatic hydrocarbon yield was 14.8 wt.%.
Example 3
The biomass used in this example was wheat straw and the industrial and elemental analyses are shown in table 2.
TABLE 2
1. Preparation of Fe/HZSM-5 catalyst
Soaking the HZSM-5 powder in a ferric nitrate nonahydrate solution at room temperature for 23 hours, drying at 79 ℃ for 11 hours, roasting at 545 ℃ for 5.5 hours, tabletting and molding, and screening out 20-40 mesh particles to obtain the Fe/HZSM-5 catalyst.
2. Preparation of bio-oil by catalytic pyrolysis
(1) Crushing corn straws, sieving the crushed corn straws with a 100-mesh sieve, and then preparing a catalyst according to the weight ratio of Fe/HZSM-5: 3, the corn stalks are: 1, mixing the two components according to the mass ratio to obtain a mixture;
(2) placing the mixture in a fixed bed pyrolysis reactor, introducing natural gas from an inlet of the fixed bed pyrolysis reactor at a gas flow rate of 10000ml/min, and carrying out catalytic pyrolysis reaction at a constant temperature of 700 ℃ and a pressure of 2Mpa for 60 min;
(3) liquid products generated by pyrolysis are carried out of the reactor along with gas, the liquid products are collected by a cold trap (-20 ℃), uncondensed gas is analyzed by Agilent gas chromatography (Agilent G1530N), and liquid products are qualitatively detected by GC-MS (Agilent 7890A/5979C). The bio-oil yield thus obtained was 41.6 wt.%, and the aromatic hydrocarbon yield was 12.3 wt.%.
Example 4
The biomass used in this example was sweet sorghum straw and the industrial and elemental analyses are shown in table 3.
TABLE 3
1. Preparation of Mo/HZSM-5 catalyst
And (2) soaking the HZSM-5 powder in an ammonium molybdate solution at room temperature for 19 hours, drying at 89 ℃ for 9 hours, roasting at 545 ℃ for 5.5 hours, tabletting and molding, and screening particles of 20-40 meshes to obtain the Mo/HZSM-5 catalyst.
2. Preparation of bio-oil by catalytic pyrolysis
(1) Crushing corn straws, sieving the crushed corn straws with a 100-mesh sieve, and then preparing a catalyst according to Mo/HZSM-5: 1, corn straw: 1, mixing the two components according to the mass ratio to obtain a mixture;
(2) placing the mixture in a fixed bed pyrolysis reactor, introducing natural gas from an inlet of the fixed bed pyrolysis reactor at a gas flow rate of 100ml/min, and carrying out catalytic pyrolysis reaction at 600 ℃ under the pressure of 1.1MPa for 400 min;
(3) liquid products generated by pyrolysis are carried out of the reactor along with gas, the liquid products are collected by a cold trap (-20 ℃), uncondensed gas is analyzed by Agilent gas chromatography (Agilent G1530N), and liquid products are qualitatively detected by GC-MS (Agilent 7890A/5979C). The bio-oil yield thus obtained was 40.5 wt.%, and the aromatic hydrocarbon yield was 8.4 wt.%.
Example 5
The biomass used in this example was corn stover, and the industrial and elemental analyses are shown in table 1.
1. Preparation of Mo/HZSM-5 catalyst
And (2) soaking the HZSM-5 powder in an ammonium molybdate solution at room temperature for 20 hours, drying at 88 ℃ for 8 hours, roasting at 540 ℃ for 5 hours, tabletting and molding, and screening particles of 20-40 meshes to obtain the Mo/HZSM-5 catalyst.
2. Preparation of bio-oil by catalytic pyrolysis
(1) Crushing corn straws, sieving the crushed corn straws with a 100-mesh sieve, and then preparing a catalyst according to Mo/HZSM-5: the corn straw is 5: 1, mixing the two components according to the mass ratio to obtain a mixture;
(2) placing the mixture in a fixed bed pyrolysis reactor, introducing methane gas from an inlet of the pyrolysis reactor at a gas flow rate of 60ml/min, and carrying out catalytic pyrolysis reaction at a constant temperature of 750 ℃ and a pressure of 0.1MPa for 30 min;
(3) liquid products generated by pyrolysis are carried out of the reactor along with gas, the liquid products are collected by a cold trap (-20 ℃), uncondensed gas is analyzed by Agilent gas chromatography (Agilent G1530N), and liquid products are qualitatively detected by GC-MS (Agilent 7890A/5979C). The bio-oil yield thus obtained was 41.9 wt.%, and the aromatic hydrocarbon yield was 14.8 wt.%.
Example 6
The biomass used in this example was corn stover, and the industrial and elemental analyses are shown in table 1.
1. Preparation of Fe/HZSM-5 catalyst
And (2) soaking the HZSM-5 powder in a ferric nitrate nonahydrate solution at room temperature for 22 hours, drying at 78 ℃ for 10 hours, roasting at 540 ℃ for 5 hours, tabletting and molding, and screening out 20-40-mesh particles to obtain the Fe/HZSM-5 catalyst.
2. Preparation of bio-oil by catalytic pyrolysis
(1) Crushing corn straws, sieving the crushed corn straws with a 100-mesh sieve, and then preparing a catalyst according to the weight ratio of Fe/HZSM-5: corn stalk is 0.8: 1, mixing the two components according to the mass ratio to obtain a mixture;
(2) placing the mixture in a fixed bed pyrolysis reactor, introducing methane gas from an inlet of the fixed bed pyrolysis reactor at a gas flow rate of 36000ml/min, and carrying out catalytic pyrolysis reaction at the constant temperature of 800 ℃ and the pressure of 3Mpa for 200 min;
(3) liquid products generated by pyrolysis are carried out of the reactor along with gas, the liquid products are collected by a cold trap (-20 ℃), uncondensed gas is analyzed by Agilent gas chromatography (Agilent G1530N), and liquid products are qualitatively detected by GC-MS (Agilent 7890A/5979C). The bio-oil yield thus obtained was 42.0 wt.%, and the aromatic hydrocarbon yield was 14.7 wt.%.
Comparative example 1
The corn stover used was the same as in example 1.
The preparation process comprises the following steps:
(1) crushing corn straws, sieving with a 100-mesh sieve, placing 5g of the crushed corn straws in a fixed bed pyrolysis reactor, introducing nitrogen from an inlet of the fixed bed pyrolysis reactor at a gas flow rate of 60ml/min, and carrying out catalytic pyrolysis reaction at a constant temperature of 750 ℃ and a pressure of 0.1MPa for 30 min;
(2) liquid products generated by pyrolysis are carried out of the reactor along with gas, the liquid products are collected by a cold trap (-20 ℃), uncondensed gas is analyzed by Agilent gas chromatography (Agilent G1530N), and liquid products are qualitatively detected by GC-MS (Agilent 7890A/5979C). The bio-oil yield thus obtained was 23.7 wt.%, and the aromatic hydrocarbon yield was 0.3 wt.%.
Comparative example 2
The corn stover used was the same as in example 1.
The preparation process comprises the following steps:
(1) crushing corn straws, sieving with a 100-mesh sieve, placing 5g of the crushed corn straws in a fixed bed pyrolysis reactor, introducing hydrogen from an inlet of the fixed bed pyrolysis reactor at a gas flow rate of 60ml/min, and carrying out catalytic pyrolysis reaction at a constant temperature of 750 ℃ and a pressure of 0.1MPa for 30 min;
(2) liquid products generated by pyrolysis are carried out of the reactor along with gas, the liquid products are collected by a cold trap (-20 ℃), uncondensed gas is analyzed by Agilent gas chromatography (Agilent G1530N), and liquid products are qualitatively detected by GC-MS (Agilent 7890A/5979C). The bio-oil yield thus obtained was 28.5 wt.%, and the aromatic hydrocarbon yield was 0.8 wt.%.
Comparative example 3
The corn stover used was the same as in example 1.
The preparation process comprises the following steps:
(1) crushing corn straws, sieving with a 100-mesh sieve, placing 5g into a fixed bed pyrolysis reactor, and introducing CH from an inlet of the fixed bed pyrolysis reactor at a gas flow rate of 60ml/min4Performing catalytic pyrolysis reaction at 750 deg.C and 0.1Mpa for 30 min;
(2) liquid products generated by pyrolysis are carried out of the reactor along with gas, the liquid products are collected by a cold trap (-20 ℃), uncondensed gas is analyzed by Agilent gas chromatography (Agilent G1530N), and liquid products are qualitatively detected by GC-MS (Agilent 7890A/5979C). The bio-oil yield thus obtained was 24.1 wt.%, and the aromatic hydrocarbon yield was 0.3 wt.%.
The above-described embodiments are merely illustrative of the preferred embodiments of the present invention, and do not limit the scope of the present invention, and various modifications and improvements of the technical solutions of the present invention can be made by those skilled in the art without departing from the spirit of the present invention, and the technical solutions of the present invention are within the scope of the present invention defined by the claims.
Claims (9)
1. A method for preparing bio-oil by coupling biomass pyrolysis and methane aromatization is characterized by comprising the following steps:
(1) crushing biomass and mixing the crushed biomass with a supported metal catalyst to obtain a mixture;
(2) in the methane atmosphere, the mixture obtained in the step (1) is subjected to catalytic pyrolysis reaction at the constant temperature of 600-800 ℃ and under the pressure of 0.1-3.0Mpa for 60-600 min;
(3) condensing and collecting the gas obtained by catalytic pyrolysis.
2. The method for preparing bio-oil by coupling biomass pyrolysis and methane aromatization according to claim 1, wherein the mass ratio of the supported metal catalyst to the biomass is (0.8-5): 1.
3. The method of claim 1, wherein the biomass comprises corn stover, wheat straw, or sweet sorghum stover.
4. The method for preparing bio-oil by coupling biomass pyrolysis and methane aromatization according to claim 1, wherein the biomass is crushed and then screened by a 100-mesh sieve.
5. The method for preparing bio-oil by coupling biomass pyrolysis and methane aromatization according to claim 1, wherein the supported metal catalyst is a Mo/HZSM-5 catalyst or a Fe/HZSM-5 catalyst.
6. The method for preparing bio-oil by using biomass pyrolysis coupled with methane aromatization according to claim 5, wherein the preparation method of the Mo/HZSM-5 catalyst comprises the following steps:
soaking the HZSM-5 powder in an ammonium molybdate solution at room temperature for 18-20 hours, drying at 88-90 ℃ for 8-10 hours, roasting at 540-550 ℃ for 5-6 hours, tabletting and molding, and screening out 20-40-mesh particles to obtain the Mo/HZSM-5 catalyst.
7. The method for preparing bio-oil by using biomass pyrolysis coupled with methane aromatization according to claim 5, wherein the preparation method of the Fe/HZSM-5 catalyst comprises the following steps:
soaking the HZSM-5 powder in a ferric nitrate nonahydrate solution at room temperature for 22-24 hours, drying at 78-80 ℃ for 10-12 hours, roasting at 540-550 ℃ for 5-6 hours, tabletting and molding, and screening out particles of 20-40 meshes to obtain the Fe/HZSM-5 catalyst.
8. The method for preparing bio-oil by coupling biomass pyrolysis and methane aromatization according to claim 1, wherein the methane atmosphere is natural gas or methane gas.
9. The method for preparing bio-oil by coupling biomass pyrolysis and methane aromatization according to claim 1, wherein the gas flow rate of the methane atmosphere is 50-36000 ml/min.
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Application publication date: 20210202 |